EP3197859B1 - Procédé de production de diesters d'acide téréphtalique avec déshydratation d'alcool recyclé - Google Patents

Procédé de production de diesters d'acide téréphtalique avec déshydratation d'alcool recyclé Download PDF

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Publication number
EP3197859B1
EP3197859B1 EP15766173.7A EP15766173A EP3197859B1 EP 3197859 B1 EP3197859 B1 EP 3197859B1 EP 15766173 A EP15766173 A EP 15766173A EP 3197859 B1 EP3197859 B1 EP 3197859B1
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alcohol
organic phase
process according
reactor
water
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EP3197859A1 (fr
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Armin Schraut
Martin KALLER
Rob BRONNEBERG
Jasmin STAMMER
Martin DAS
Gerrit HARNISCHMACHER
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BASF SE
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BASF SE
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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C67/00—Preparation of carboxylic acid esters
    • C07C67/08—Preparation of carboxylic acid esters by reacting carboxylic acids or symmetrical anhydrides with the hydroxy or O-metal group of organic compounds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/18—Stationary reactors having moving elements inside
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C69/00—Esters of carboxylic acids; Esters of carbonic or haloformic acids
    • C07C69/76—Esters of carboxylic acids having a carboxyl group bound to a carbon atom of a six-membered aromatic ring
    • C07C69/80—Phthalic acid esters
    • C07C69/82—Terephthalic acid esters
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00051—Controlling the temperature
    • B01J2219/00132—Controlling the temperature using electric heating or cooling elements

Definitions

  • the invention relates to a process for the preparation of terephthalic diesters by reacting terephthalic acid with at least one alcohol.
  • Esters of terephthalic acid are used as plasticizers and are characterized by favorable toxicological properties.
  • carboxylic acid esters by reacting carboxylic acids with alcohols. This reaction can be carried out autocatalytically or catalytically, for example by Brönstedt or Lewis acids. Regardless of the type of catalysis, there is always a temperature-dependent equilibrium between the starting materials (carboxylic acid and alcohol) and the products (esters and water).
  • an entraining agent is generally used, with the aid of which the water of reaction is removed from the batch. If one of the starting materials (alcohol or carboxylic acid) boils lower than the formed ester and forms a miscibility gap with water, an educt can be used as entraining agent and be recycled after separation of water in the approach.
  • the alcohol used is usually the entraining agent.
  • the alcohol used as the entraining agent it is customary to at least partially condense the vapors from the reactor, to separate the condensate into an aqueous phase and an organic phase essentially consisting of the alcohol used for the esterification, and at least partially separate the organic phase returns to the reactor.
  • the EP-A 1 186 593 describes a process for the preparation of carboxylic acid esters by reaction of di- or polycarboxylic acids or their anhydrides with alcohols, wherein the water of reaction is removed by azeotropic distillation with the alcohol. The amount of liquid removed from the reaction by the azeotropic distillation is completely or partially replenished with the alcohol.
  • the WO 2010/076192 A1 proposes to remove low boilers from the organic phase to be recycled in order to prevent their accumulation in the reactor system.
  • the US 7,276,621 B2 describes a process for the titanate-catalyzed esterification of terephthalic acid with 2-ethylhexanol. An inert gas is passed through the reaction mixture to aid in the removal of water.
  • JP 4956945 B2 describes a process for the esterification of terephthalic acid with 2-ethylhexanol.
  • the terephthalic acid is introduced as a slurry continuously or discontinuously into the reaction system.
  • the metered addition takes place in the same speed, in which the terephthalic acid is converted to the product.
  • the US 7,799,942 B2 describes a process for preparing terephthalic diesters in a reactor at atmospheric pressure using a distillation column placed on top of the reactor. In addition, the reaction mixture is flowed through by an inert gas.
  • the WO 2010/076193 A1 describes a process for the purification of the crude ester product of an esterification reaction in which a metal-containing esterification catalyst is used.
  • US 2,825,738 A discloses the esterification of a suspension of terephthalic acid with methanol in which the mixture of methanol and water is distilled off and separated. The anhydrous methanol thus obtained is recycled to the reaction system.
  • terephthalic acid in higher alcohols is low.
  • terephthalic acid in 2-ethylhexanol at 180 ° C is only less than 0.65 wt .-% soluble.
  • the reaction of terephthalic acid with higher alcohols proceeds via the part of terephthalic acid dissolved in the alcohol.
  • it is essential to ensure a constant mixing of the heterogeneous mixture of terephthalic acid and alcohol and an effective heat input into the reaction system.
  • the invention is therefore based on the object to provide a process for the preparation of terephthalic acid diesters, which allows a simple entry of terephthalic acid into the reactor and reaches a complete conversion of terephthalic acid.
  • Another object of the invention is to provide a process that can be carried out in existing reactors for esterification reactions by minor conversions.
  • the process according to the invention can be carried out batchwise or continuously, but is preferably carried out batchwise.
  • the process obviates the problems associated with metering solid terephthalic acid into the reactor, such as clumping of the terephthalic acid and clogging of the screw conveyor or other conveyor.
  • the process provides for the preparation of a presuspension in a dispersing kettle.
  • Terephthalic acid is not metered as a solid but in the form of a suspension in the reactor.
  • terephthalic acid is suspended in the dispersing kettle in a portion of the alcohol.
  • a suitable mixing device is used.
  • an amount of terephthalic acid can be mixed with an agitator with alcohol, alternatively, dispersing pumps can be used.
  • the entire amount of terephthalic acid can be suspended in one step or in the course of the process, the terephthalic acid are suspended in portions.
  • terephthalic acid can be metered into the dispersing kettle, for example with the aid of a screw conveyor.
  • the mixing can also be carried out in a closed chamber by the interaction of a rotating rotor and a stator, wherein continuously only one incremental amount of the components is mixed with each other, and the suspension then emerges from the chamber.
  • the alcohol for preparing the pre-suspension at least partially dehydrated back alcohol is used, i. the organic phase obtained after condensation of the vapor, phase separation of the condensate and dehydration of the organic phase.
  • fresh alcohol can be used for the initial preparation of the pre-suspension for starting the process.
  • the dispersing boiler is usually made of metallic materials, with stainless steel being preferred.
  • the dispersing boiler can be connected to the reactor on the gas side.
  • the pre-suspension can be passed with a pump in the reactor.
  • the pre-suspension can also be conducted by gravity into the reactor.
  • all pumps known to those skilled in the art can be used as pumps, which the latter considers suitable taking into account the properties of the presuspension to be conveyed.
  • a centrifugal, piston, screw, impeller or peristaltic pump can be used as a feed pump.
  • the addition of the pre-suspension in the reactor can be carried out in portions or continuously. Preferably, the metered addition is carried out continuously.
  • the pre-suspension can in principle be metered in at any point of the reactor, but preferably the pre-suspension is added in the upper region of the reactor, in particular above the liquid level in the reactor. In this way, reverse flow against the metering direction can be largely prevented.
  • the reactor may be any reactor suitable for carrying out chemical reactions in the liquid phase.
  • Suitable reactors are non-backmixed reactors, such as tubular reactors or built-in residence time vessels, but preferably backmixed reactors, such as stirred tanks, loop reactors, jet loop reactors or jet nozzle reactors.
  • backmixed reactors such as stirred tanks, loop reactors, jet loop reactors or jet nozzle reactors.
  • several reactors can be combined in a multi-stage apparatus.
  • Such reactors are, for example, loop reactors with built-in sieve trays, cascaded vessels, tube reactors with intermediate feed or stirred columns.
  • Roughkesselreaktoren usually consist of metallic materials, with stainless steel is preferred.
  • the pre-suspension and the esterification catalyst are brought into contact to obtain a reaction suspension.
  • i) the pre-suspension is passed into the unfilled reactor, ii) the boiling suspension is boiled and iii) the esterification catalyst is added.
  • the order of steps ii) and iii) may be reversed.
  • the esterification catalyst is reacted in a partial amount of alcohol, e.g. 15-50% of the total amount of alcohol, preferably 25-40%, presented in the reactor.
  • the catalyst / alcohol mixture can first be heated to boiling and then the addition of the pre-suspension can be started.
  • the presuspension is added to the catalyst / alcohol mixture and then heated.
  • the heating of the catalyst / alcohol mixture and the addition of the pre-suspension can be carried out in parallel.
  • Particularly preferred is the metered addition of the catalyst in the heated to boiling in the reactor pre-suspension.
  • the heating of the initially introduced alcohol, the pre-suspension and / or a catalyst / alcohol mixture in the reactor can be effected in any desired manner, for example by using a heating medium in a jacketed vessel, by electroheating, by pumping the mixture introduced via an external heat exchanger or by an internal heating register , which is heated using a heating medium, such as steam or oil.
  • a heating medium such as steam or oil.
  • the heat input into the reaction system can take place.
  • the reaction suspension is heated by pumping it over a heat exchanger located outside the reactor.
  • heat exchangers in principle, all known heat exchangers, for example plate or tube bundle heat exchangers, or combinations thereof into consideration.
  • the reaction suspension is withdrawn from the reactor using a pump and passed through the heat exchanger.
  • the heat exchanger is for the return of the heated reaction suspension in the Reactor fluidly connected to the reactor.
  • the reaction suspension may in principle be withdrawn at different positions of the reactor below the liquid level of the reaction suspension, but preferably the reaction suspension is withdrawn at the lowest point of the reactor.
  • the reactor is designed so that the reaction suspension is withdrawn at the geodesic lowest point of the reactor and no dead spaces, due to locally deepest points, are present in the reactor.
  • the pump for withdrawing the reaction suspension can in principle be arranged at different positions outside the reactor. For example, the pump is located at the geodetically lowest point of the circuit consisting of reactor, pump and connecting lines.
  • feed pumps in principle all known in the art feed pumps are suitable, which considers this for carrying out the method according to the invention, taking into account the properties of the reaction suspension to be conveyed suitable.
  • a centrifugal, piston, screw, impeller or peristaltic pump can be used as a feed pump.
  • a feed pump preferably, a centrifugal, piston, screw, impeller or peristaltic pump.
  • a centrifugal, piston, screw, impeller or peristaltic pump can be used as a feed pump.
  • a centrifugal, piston, screw, impeller or peristaltic pump can be used as a feed pump.
  • axial or radial centrifugal pump Very particular preference is given to an axial or radial centrifugal pump.
  • the return of the reaction suspension in the reactor can in principle be carried out at any position of the reactor, but expediently the recirculation takes place in the upper region of the reactor, for example at the level of the liquid level of the reaction suspension or in the range from the height of the liquid level of the reactor suspension to 30% below.
  • the volumetric flow which is conducted through the heating device is selected, for example, such that a circulation of the complete reactor contents takes place in a period of 1 to 60 minutes, preferably 1 to 10 minutes. Constant circulation of the reactor contents ensures effective mixing of the reaction suspension.
  • the circulation of the reaction suspension can be assisted by metering in an inert gas into the reactor, in particular at the lowest point of the reactor, and / or a stream of the reaction suspension.
  • the metering of the inert gas contributes, in particular in case of malfunction of the pump for the removal of the reaction suspension, for example in case of failure of the pump, to prevent sedimentation of terephthalic acid at the reactor bottom or in pipelines.
  • the dosing of the inert gas takes place on the suction side of the pump.
  • the metering can be done on the pressure side of the pump.
  • Inert gases are all gases which, under the reaction conditions, have no reactivity with the constituents of the reaction suspension, in particular nitrogen or argon.
  • the inert gas is introduced in an amount of 0.01 to 5 volume units of the inert gas per unit volume of the reaction suspension per hour.
  • the mixing can be assisted by the use of a stirrer.
  • the reaction suspension in the reactor has a temperature near the boiling point of the reaction mixture, for example, a temperature of 150 ° C to 250 ° C, preferably 185 ° C to 220 ° C.
  • the boiling point of the reaction suspension is dependent on the ratio of terephthalic acid to alcohol and increases in the course of the reaction. Boiling alcohol in the reaction suspension causes density differences, due to which the reaction suspension is circulated and circulated in the reactor.
  • an alcohol-water azeotrope is distilled off with the vapor, the vapor is at least partially condensed, the condensate is separated into an aqueous phase and an organic phase.
  • capacitors For condensation or partial condensation of the vapor all suitable capacitors can be used. These can be cooled with any cooling media. Capacitors with air cooling and / or water cooling are preferred, with air cooling being particularly preferred.
  • the resulting condensate is subjected to phase separation into an aqueous phase and an organic phase.
  • the condensate is passed for this purpose in a phase separator (decanter), where it decays by mechanical settling into two phases, which can be deducted separately.
  • the aqueous phase is separated off and, if appropriate after work-up, can be discarded or used as stripping water in the after-treatment of the ester.
  • the separated organic phase contains according to the thermodynamic solubility of water in the alcohol still dissolved water and is dehydrated before further use.
  • the dehydration of the organic phase can be carried out in various ways, for example by pervaporation using membranes ( JP-A-04308543 ), azeotropic distillation in the presence of an entrainer, such as cyclohexane, treatment with molecular sieves or zeolites ( EP-A-205 582 . GB-A-2151501 . EP-A-142157 . EP-A-158754 . US-A-4407662 . US-A-4372857 . GB-A-2088739 and FR-A-2719039 ) or the use of a combination of extraction with liquid carbon dioxide and a molecular sieve and then fractional distillation ( EP-A-233692 ).
  • an entrainer such as cyclohexane
  • molecular sieves capable of adsorbing dissolved water from an alcohol are well known. Typically, such molecular sieves are crystalline.
  • the molecular sieve is suitably a zeolite molecular sieve having an average pore diameter of about 3 Angstroms. Typical examples of such molecular sieves are the zeolites type A, in particular 3A, 4A and 5A.
  • the dewatering of the organic phase comprises stripping with alcohol vapor.
  • the organic phase is passed, optionally after alcohol enrichment, in the upper region of a stripping column and treated with alcohol vapor in countercurrent.
  • Suitable as a stripping column are in particular tray columns, packed columns or packed columns.
  • the alcohol vapor is suitably produced by a heater, which is fluid-conductively connected to the bottom of the stripping column.
  • a gaseous water / alcohol mixture is withdrawn. It is possible to at least partially condense the gaseous water / alcohol mixture, to separate the condensate into an aqueous phase and an organic phase, and to pass the organic phase at least partially as reflux into the stripping column and / or into the reactor.
  • the gaseous water / alcohol mixture from the top of the stripping column and the Christsbrüden to a common workup, using a common capacitor and phase separator.
  • the organic phase is made to exhaust the vapor from the reactor to obtain an alcohol-enriched organic phase and strip the alcohol-enriched organic phase in a stripping column with alcohol vapor to obtain the dewatered organic phase ,
  • the alcohol vapor is suitably produced by a heater, which is fluid-conductively connected to the bottom of the stripping column.
  • the gaseous water / alcohol mixture from the stripping column is suitably passed to the lower part of the stripping column. At the top of the reinforcing column, a gaseous water / alcohol mixture is withdrawn.
  • the gaseous water / alcohol mixture is at least partially condensed, the condensate is separated into an aqueous phase and an organic phase, and at least passes the organic phase partly as reflux into the sparing column and / or the stripping column.
  • the embodiment allows for optimal heat integration of the process. To operate the boiler of the stripping column, steam of a lower steam level is sufficient than for heating the reaction suspension.
  • the amplification column is preferably arranged directly on the reactor.
  • an alcohol-enriched organic phase is collected in the lower part of the reinforcing column.
  • a collecting tray is suitably mounted in the lower part of the column, for. B. a fireplace floor with equally distributed roofed fireplaces.
  • the collecting tray has e.g. a gradient to the inside and a central trigger cup and vent on. From the collecting bottom of the column, the collected alcohol-enriched organic phase is passed into the stripping column.
  • the derivation of the back alcohol can be done by gravity or by using a pump, preferably by gravity.
  • the stripping column is preferably located outside the reactor and fluidly connected to the withdrawal of the sparing column.
  • the stripping column and the reinforcing column can also be in the form of a one-piece rectification column, with the reaction mixture being fed laterally into the central region of the column.
  • the organic phase is freed from traces of water that remain after the phase separation in the organic phase or are dissolved according to their thermodynamic solubility in the organic phase.
  • the water content in the dewatered organic phase is usually lower than the solubility of water in the alcohol, but is preferably less than 1000 ppm, especially less than 100 ppm.
  • the dehydration of the organic phase has the advantage that the water content in the reaction mixture is kept low, so that the reaction equilibrium can be shifted to the product side and, if hydrolysis-sensitive esterification catalysts are used, the hydrolysis of the catalyst can be prevented.
  • the dewatered organic phase is passed at least partially into the dispersing kettle.
  • the dehydrated organic phase can be passed directly into the dispersing or alternatively initially passed into a heated and / or insulated reservoir, stored there and passed from there into the dispersing.
  • the preheating of the dehydrated organic phase in the reservoir has the advantage that energy losses can be avoided by cooling, for heating low pressure steam can be used and the solubility of terephthalic acid in warm alcohol is significantly greater than in cold.
  • the dehydrated organic phase in the reservoir is heated to a temperature below the boiling point of the alcohol, in particular to a temperature of 50 ° C to 10 ° C below the boiling point of the alcohol.
  • the heat input into the reservoir can be done in any way, for. B. by an outboard heating jacket and / or internal heating coils which are heated by means of a heating medium, or an electric heating or by pumping through an external heat exchanger.
  • the derivation of the organic phase from the rectification device, as well as from the reservoir into the dispersing vessel, can be accomplished by gravity or using a conveyor, e.g. a centrifugal, piston, screw, impeller or peristaltic pump done.
  • a conveyor e.g. a centrifugal, piston, screw, impeller or peristaltic pump done.
  • the organic phase passed, optionally after storage in the heated storage tank, into the dispersing kettle is available for the suspension of terephthalic acid in the dispersing kettle.
  • the dosage of terephthalic acid as a pre-suspension can be distributed over the duration of the reaction. This eliminates the need to handle concentrated suspensions.
  • This has the advantage that the suspension supplied to the reactor has a low solids content and thus can be well promoted. Furthermore, by the use of back alcohol, the solids concentration in the reactor is also low, whereby the reaction volume can be used optimally. Another advantage is that fewer problems occur due to sedimentation in case of failure of the conveyor.
  • linear, branched or cyclic aliphatic alcohols having 8 to 14 C atoms, or aromatic alcohols.
  • the alcohols are monools and may be tertiary, secondary or primary.
  • the alcohols used can come from different sources. Suitable starting materials are, for example, fatty alcohols, alcohols from the Alfol process or alcohols or alcohol mixtures which have been obtained by hydrogenation of saturated or unsaturated aldehydes, in particular those whose synthesis includes a hydroformylation step.
  • Aliphatic alcohols which are used in the process according to the invention are, for example, octanols, such as n-octanol, 2-ethylhexanol, nonanols, decyl alcohols or tridecanols prepared by hydroformylation or aldol condensation and subsequent hydrogenation.
  • the alcohols can be used as a pure compound, as a mixture of isomeric compounds or as a mixture of compounds with different carbon numbers.
  • An example of such an alcohol mixture is a C 9 / C 11 alcohol mixture.
  • Aromatic alcohols which can be used in the process according to the invention are, for example, phenol, benzyl alcohol, 1-naphthol, 2-naphthol, 2,4,6-trinitrophenol, primary phenylethyl alcohol, secondary phenylethyl alcohol, phenylpropyl alcohol, o-tolyl alcohol, p-tolyl alcohol, cumene alcohol , p-nitrophenol, m-, o- or p-alkylphenol, eg m-, o- or p-methylphenol or m-, o- or p-ethylphenol, m-, o- or p-halophenol, e.g.
  • Particularly preferred alcohols are 2-ethylhexanol, 2-propylheptanol, isononanol isomer mixtures, decanol isomer mixtures and C 9 / C 11 -alcohol mixtures.
  • the alcohol to be converted which serves as an entraining agent, can be used in stoichiometric excess.
  • the amount of alcohol used is chosen so that in the crude product of the reaction 10 to 35 wt .-% alcohol, based on the theoretical full conversion of terephthalic acid.
  • the esterification according to the invention is carried out in the presence of an esterification catalyst.
  • the esterification catalyst is soluble in the alcohol.
  • the esterification catalyst is among Lewis acids such as alcoholates, carboxylates and chelate compounds of titanium, zirconium, hafnium, tin, aluminum and zinc; Boron trifluoride, boron trifluoride etherates; Mineral acids, such as sulfuric acid, phosphoric acid; Sulfonic acids, such as methanesulfonic acid and toluenesulfonic acid, and ionic fluids.
  • Lewis acids such as alcoholates, carboxylates and chelate compounds of titanium, zirconium, hafnium, tin, aluminum and zinc
  • Boron trifluoride such as sulfuric acid, phosphoric acid
  • Sulfonic acids such as methanesulfonic acid and toluenesulfonic acid, and ionic fluids.
  • the esterification catalyst is selected from alcoholates, carboxylates and chelate compounds of titanium, zirconium, hafnium, tin, aluminum and zinc.
  • Tetraalkyl titanates such as tetramethyl titanate, tetraethyl titanate, tetra-n-propyl titanate, tetra-isopropyl titanate, tetra-n-butyl titanate, tetra-isobutyl titanate, tetrasec-butyl titanate, tetraoctyl titanate, tetra (2-ethylhexyl) titanate; Dialkyl titanates ((RO) 2 TiO, where R is, for example, isopropyl, n-butyl, iso-butyl), such as isopropyl n-butyl titanate; Titanium acetylacetonate chelates such as di-isopropoxy-bis (acetylacetonate)
  • Suitable ionic liquids are z.
  • the catalyst concentration depends on the type of catalyst. In the titanium compounds preferably used, this is 0.001 to 1.0 mol% based on the amount of terephthalic acid, in particular from 0.01 to 0.2 mol%.
  • the reaction temperatures are generally between 100 ° C and 250 ° C. The optimum temperatures depend on the starting materials, reaction progress and the catalyst concentration. They can easily be determined by experiment for each individual case. Higher temperatures increase the reaction rates and promote side reactions, such as olefin formation or formation of colored By-products. It is necessary to remove the water of reaction that the alcohol can distill off from the reaction mixture.
  • the desired temperature or the desired temperature range can be adjusted by the pressure in the reactor. In the case of low-boiling alcohols, therefore, the reaction can be carried out under reduced pressure and with higher-boiling alcohols under reduced pressure. For example, in the reaction of terephthalic acid with 2-ethylhexanol in a temperature range of 180 ° C to 220 ° C in the pressure range of 300 mbar to 2 bar worked.
  • the reactor and dispersing vessel are operated at substantially the same pressure, in particular approximately ambient pressure.
  • reactor and dispersing vessel can also be operated at different pressures.
  • the process of the invention is carried out until the terephthalic acid is substantially completely reacted.
  • the determination of the conversion can be made by determining the acid number of the reaction suspension.
  • the acid number is determined by neutralization of a sample of the reaction suspension with tetrabutylammonium hydroxide.
  • the amount of tetrabutylammonium hydroxide consumed can be determined via the mass of tetrabutylammonium hydroxide consumed in the neutralization, and the amount of free acid groups of unconverted terephthalic acid is determined stoichiometrically. Based on the known amount of terephthalic acid used, the conversion can be determined. Additional possibilities for determining the conversion are HPLC measurements and the measurement of the turbidity of the reaction suspension by in-line haze measurements. In the process according to the invention, preferably a conversion greater than 99% is achieved.
  • reaction mixture which consists essentially of the desired ester and excess alcohol, in addition to the catalyst and / or its derivatives small amounts of ester carboxylic acid (s) and / or unreacted carboxylic acid.
  • the esterification catalyst is deactivated by addition of an aqueous base and precipitated. At the same time, the unreacted in the esterification reaction acid or partial ester of the acid are converted into salts.
  • aqueous base may be effected in any suitable manner. It is preferably carried out below the liquid surface of the crude ester.
  • z. As lances or nozzles, which are provided on a container bottom or the container wall. The mixture is then mixed thoroughly, z. B. by means of a stirrer or a circulating pump.
  • the amount of aqueous base added is such that it is sufficient to completely neutralize the acid components of the crude ester. In practice, a more or less large excess of base is used.
  • the total amount of the acidic components of the crude ester is conveniently measured by the acid number (in mg KOH / g).
  • 100 to 300% neutralization equivalents are introduced with the aqueous base, based on the acid number of the crude ester, in particular 130 to 220%.
  • neutralization equivalent is meant the amount of base capable of binding the same number of protons as 1 mg of KOH. In other words, one uses a base excess of up to 200%, preferably 30 to 120%.
  • Suitable aqueous bases are solutions of hydroxides, carbonates, bicarbonates of alkali metals and alkaline earth metals.
  • Aqueous alkali metal hydroxide solutions are generally preferred.
  • Aqueous sodium hydroxide solution is particularly preferred because of its ready availability.
  • the concentration of the aqueous base is not critical per se, but the use of concentrated alkali solutions at the point of introduction of the base may result in the hydrolysis of the esters.
  • the concentration of the aqueous base should not be too low, since the water introduced with the aqueous base must be removed again in the subsequent step. Therefore, aqueous bases of moderate to low concentration are preferred, e.g. B. those of a concentration of 0.5 to 25 wt .-%, in particular 1 to 10 wt .-%.
  • Aqueous sodium hydroxide solution with a concentration of 1 to 5 wt .-% is particularly preferred.
  • the precipitated solid consisting essentially of catalyst decomposition products and salts of unreacted acid or partial esters of polybasic acids, is present in finely divided, difficult to filter form. Conveniently, the fine particles are agglomerated into larger, easily separable particles.
  • the liquid phase is added to form a water-in-oil emulsion with water.
  • the water is distributed as a disperse phase in the form of fine droplets in the liquid organic phase.
  • the fine particulates migrate to the interface between water droplets and surrounding organic phase.
  • the fine particles agglomerate and form coarse, easily separable particles.
  • the added amount of water In order for its own water phase to form, the added amount of water must be greater than the solubility of water in the organic phase corresponds.
  • the water solubility in the organic phase depends inter alia on the content of unreacted alcohol, since the alcohol acts as a solubilizer. The higher the alcohol content, the more water must be added to form the emulsion. In the case of customary residual alcohol contents of from 20 to 30% by weight, amounts of from 10 to 80 g of water, preferably from 30 to 50 g, based on 1 kg of crude ester, are generally suitable.
  • the water phase is broken up into fine droplets using a suitable stirrer or homogenizer or by pumping the emulsion over using a circulation pump.
  • the water droplets produced preferably have an average droplet size of less than 1000 microns.
  • stirrers with high specific stirring power for example, disk stirrers are suitable.
  • the emulsion is conveniently carried out at about atmospheric pressure.
  • the solid is in a good filterable form; it does not precipitate fines in the filtration.
  • suitable filters such as chamber filter presses, band filter, candle filter or plate filter.
  • plate filter For continuous process control are particularly plate filter with Zentrifugalkuchenabmine. The separated solid is discarded.
  • the ester may be subjected to various post-treatments, such as steam stripping or the like.
  • FIG. 1 shows a suitable for carrying out the process according to the invention plant.
  • Terephthalic acid from the reservoir 10 is metered into a dispersing vessel 7 and dispersed in alcohol using a stirrer 11 to obtain a pre-suspension.
  • alcohol is metered from the reservoir 9 into the dispersing vessel 7.
  • the pre-suspension is passed by means of a pump 8 in the upper region of the reactor 1.
  • the reactor 1 are another subset of the alcohol and the esterification catalyst.
  • the reaction suspension is withdrawn from the reactor using a pump 2 and passed through heat exchanger 3.
  • the reaction suspension heated in the heat exchanger 3 is returned to the upper area of the reactor 1 again.
  • the vapor passes through the reinforcing column 6 and is at least partially condensed in the condenser 4.
  • the condensate is separated into an aqueous and an organic phase.
  • the aqueous phase is discarded, the organic phase is passed as reflux into the reinforcing column 6.
  • the organic phase can be passed into the stripping column 12.
  • an alcohol-enriched organic phase is collected and passed into the stripping column 12.
  • the stripping column 12 comprises a sump heater which partially vaporizes the organic phase. Due to the ascending alcohol vapors traces of water are stripped from the alcohol-enriched organic phase. Alcohol-water vapors are withdrawn overhead and passed into the lower region of the booster column 6 and / or the condenser 4. Bottom liquid from the stripping column 12 is either passed directly via line 14 into the dispersing vessel 7 or temporarily stored in the reservoir 13.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Claims (13)

  1. Procédé de fabrication d'un diester de l'acide téréphtalique par mise en réaction d'acide téréphtalique avec au moins un alcool, selon lequel
    a) de l'acide téréphtalique est suspendu dans l'alcool dans une cuve de dispersion, une pré-suspension étant obtenue,
    b) la pré-suspension est acheminée depuis la cuve de dispersion dans un réacteur et mise en réaction en présence d'un catalyseur d'estérification, et
    c) l'eau de réaction est éliminée par distillation sous la forme d'un azéotrope alcool-eau avec les vapeurs, les vapeurs sont au moins partiellement condensées, le condensat est séparé en une phase aqueuse et une phase organique, la phase organique est déshydratée et la phase organique déshydratée est au moins partiellement acheminée dans la cuve de dispersion,
    et l'alcool est choisi parmi les mono-alcools aliphatiques en C8 à C14 linéaires, ramifiés ou cycliques ou les mono-alcools aromatiques.
  2. Procédé selon la revendication 1, dans lequel la phase organique déshydratée présente une teneur en eau inférieure à 1 000 ppm.
  3. Procédé selon la revendication 1 ou 2, dans lequel la phase organique est déshydratée par extraction avec une vapeur d'alcool.
  4. Procédé selon la revendication 3, dans lequel la phase organique est mise en circulation à contre-courant des vapeurs dans une colonne d'enrichissement afin d'obtenir une phase organique enrichie en alcool, et la phase organique enrichie en alcool est extraite dans une colonne de rectification avec une vapeur d'alcool afin d'obtenir la phase organique déshydratée.
  5. Procédé selon l'une quelconque des revendications précédentes, dans lequel la phase organique déshydratée est stockée dans un contenant isolé et/ou chauffé avant l'introduction dans la cuve de dispersion.
  6. Procédé selon l'une quelconque des revendications précédentes, dans lequel le catalyseur d'estérification est choisi parmi les acides de Lewis, les acides minéraux, les acides sulfoniques et les fluides ioniques.
  7. Procédé selon la revendication 6, dans lequel le catalyseur d'estérification est choisi parmi les alcoolates, les carboxylates et les composés chélatés de titane, de zirconium, d'étain, d'hafnium, d'aluminium et de zinc ; le trifluorure de bore, les éthérates de trifluorure de bore ; l'acide sulfurique, l'acide phosphorique ; l'acide méthanesulfonique et l'acide toluènesulfonique.
  8. Procédé selon les revendications 1 à 7, dans lequel le catalyseur d'estérification est choisi parmi les échangeurs d'ions acides, les zéolithes, les oxydes et/ou hydroxydes de magnésium, d'aluminium, de zinc, de titane, de silicium, d'étain, de plomb, d'antimoine, de bismuth, de molybdène et de manganèse.
  9. Procédé selon l'une quelconque des revendications précédentes, dans lequel le catalyseur d'estérification est soluble dans l'alcool.
  10. Procédé selon l'une quelconque des revendications précédentes, dans lequel l'alcool est utilisé en un excès stoechiométrique tel que le produit d'estérification brut contient 15 à 35 % en poids d'alcool.
  11. Procédé selon l'une quelconque des revendications précédentes, dans lequel un gaz inerte est introduit dans le réacteur et/ou un courant de la suspension de réaction pour la fluidisation.
  12. Procédé selon l'une quelconque des revendications précédentes, dans lequel, pour le traitement, le diester de l'acide téréphtalique brut est mélangé avec une base aqueuse, l'eau est évaporée du mélange obtenu, la phase liquide obtenue est mélangée avec de l'eau pour obtenir une émulsion eau dans huile, l'eau est éliminée par distillation de l'émulsion et le diester de l'acide téréphtalique est filtré.
  13. Procédé selon l'une quelconque des revendications précédentes, dans lequel la suspension de réaction est chauffée par pompage dans un échangeur de chaleur.
EP15766173.7A 2014-09-24 2015-09-21 Procédé de production de diesters d'acide téréphtalique avec déshydratation d'alcool recyclé Active EP3197859B1 (fr)

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CN112439377A (zh) * 2019-08-29 2021-03-05 江苏察克润滑科技有限公司 一种用于制备防锈液的反应釜
KR102501597B1 (ko) * 2019-09-25 2023-02-20 주식회사 엘지화학 디에스테르계 조성물의 제조 시스템 및 제조방법
KR102683132B1 (ko) * 2019-09-27 2024-07-10 주식회사 엘지화학 디에스터계 물질의 정제 유닛 및 이를 포함하는 디에스터계 물질의 정제 시스템
KR20220067385A (ko) * 2020-11-17 2022-05-24 주식회사 엘지화학 디에스터계 화합물의 제조방법
CN115282894A (zh) * 2022-06-30 2022-11-04 福建久策气体股份有限公司 一种二氟乙酰乙酸乙酯生产装置及其工作方法

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MX2017003920A (es) 2017-06-28
ES2724982T3 (es) 2019-09-18
BR112017005839A2 (pt) 2018-01-30
EP3197859A1 (fr) 2017-08-02
RU2668223C1 (ru) 2018-09-27
WO2016046118A1 (fr) 2016-03-31
CA2962305A1 (fr) 2016-03-31
US10207978B2 (en) 2019-02-19
US20170297997A1 (en) 2017-10-19
TR201904928T4 (tr) 2019-05-21
CA2962305C (fr) 2019-06-11
CN106715382A (zh) 2017-05-24
PL3197859T3 (pl) 2019-08-30
TW201612150A (en) 2016-04-01

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